US4547201A - SRC Residual fuel oils - Google Patents
SRC Residual fuel oils Download PDFInfo
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- US4547201A US4547201A US06/561,388 US56138883A US4547201A US 4547201 A US4547201 A US 4547201A US 56138883 A US56138883 A US 56138883A US 4547201 A US4547201 A US 4547201A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
- C10L1/00—Liquid carbonaceous fuels
- C10L1/32—Liquid carbonaceous fuels consisting of coal-oil suspensions or aqueous emulsions or oil emulsions
- C10L1/322—Coal-oil suspensions
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- This invention relates to a composition of matter which has utility as a fuel oil substitute.
- this invention relates to a blend of solvent refined coal in a mixture of distillate oils.
- the resulting composition exhibits long term stability as a fuel oil and it may be used with only minor modification in existing infrastructures.
- Coal refining consists of adding hydrogen to coal and removing its principal pollutants, sulphur and ash.
- raw coal is pulverized, mixed with a solvent derived from the refining process and heated under pressure.
- Hydrogen is added and the hydrogenated coal-solvent mixture is sent to a reactor vessel where liquefaction occurs.
- the resulting mixture is passed to a separator, naphtha and distillate liquids are drawn off, sulphur is removed as hydrogen sulphide and ash is eliminated by a conventional deashing step.
- the principal product of this operation is solvent refined coal, that is, SRC which at ambient temperature is a shiny, black solid.
- SRC solvent refined coal
- TSL SRC a solid residual fuel having very low sulphur content and more naphtha and distillate liquids.
- compositions comprised of solvent refined coal and distillate oils have been reported in the literature but their use as fuel oil substitutes has not been widely accepted due to their instability over the long term. It has heretofore been believed that the asphaltenes and preasphaltenes content of the SRC would always result in an unstable mixture of SRC and coal derived liquids.
- J. Schiller describes a simulated fuel oil comprised of finely ground distillation residues derived from SRC and anthracene oils. These compositions exhibit a low viscosity which Schiller attributes to the synergistic effect of asphaltene on anthracene oil.
- Asphaltenes are polar compounds which are found in distillation residues. They are high in heteroatom content and they possess hydroxy and nitrogen moieties which contribute to the formation of insoluble residues; however, Schiller observed, surprisingly, that the synergistic effect of asphaltene resulted in a composition free of undissolved solids. Unfortunately, however, the distillation residues in these liquids do not remain in solution indefinitely and, therefore, the synergistic effect of asphaltene cannot explain fully the undissolved solids which have been observed over extended storage periods.
- FIGS. 1-6 graphically depict the viscosity characteristics of solvent refined coal-distillate oil blends as well as the viscosity characteristics of No. 6 fuel oil in relation to temperature and storage time.
- deashed solvent refined coal SRC or TSL SRC
- ⁇ SRC ⁇ is used herein to jointly and severally refer to the various sources of non-distillate solvent-refined coal products, nominally, 850° F.+ coal, for example, SRC, HSRC and TSL SRC.
- a unique feature of this invention lies in the discovery that a correlation exists between the homogeneity of SRC fuel oil and the heteroatom composition of the distillate oils and the particular SRC which are mixed.
- SRC solids for example, are rich in nitrogen, oxygen and sulphur, that is, heteroatoms which exert a high degree of polarity within the molecule.
- a contributor to this effect are the preasphaltenes which are present in solvent refined coal in appreciable amounts.
- the preasphaltenes are pyridine solubles rich in polar functional groups and it has been found that solubilization of SRC requires solvents having a polarity at least equal to or greater than pyridine.
- This invention provides guidelines for optimizing the solubility of SRC solids in distillate oils. It identifies the polarity requirement of the solvent necessary to form homogeneous residual oil blends and specifies the compositions of heteroatom rich first-stage oil to be added to make SRC and second-stage oil homogeneous blends.
- this invention relates to a homogeneous, single-phase blend of fuel oil consisting essentially of deashed solvent-refined coal and distillate oils derived from the liquefaction of coal, said oils having a heteroatom content greater than about 25 wt% of the heteroatom content of said solvent-refined coal.
- distillate oils employed in this invention are first- and second-stage distillate oils having a boiling range of 400°-1000° F.; they are comprised nominally of 400°-650° F. middle oil, 650°-850° F. heavy oil and 450°-850° F. process solvent. These distillate oils can be used individually or they can be used in various combinations with deashed SRC to provide a homogeneous single-phase SRC residual oil blend having viscosity-temperature characteristics which make it suitable for use of substitute for No. 6 fuel oil.
- the amount of distillate oil combined with deashed solvent-refined coal depends upon the heteroatom content of the distillate oil employed. At concentrations equal to or greater than 40 wt% deashed solvent refined coal cannot be mixed even at temperatures close to its flash point to form homogeneous blends with middle oil, heavy oil or process solvent of the second stage.
- first stage distillate oils contain the greatest concentration of heteroatoms and, therefore, deashed solvent-refined coal (SRC) forms homogeneous blends with first-stage distillate oils at all concentrations.
- SRC deashed solvent-refined coal
- homogeneous blends of SRC (above 40 wt%) and second-stage middle oil require the addition of first-stage heavy oil in quantities greater than 15 wt%.
- a homogeneous blend of SRC and second-stage heavy oil can be made only if first-stage heavy oil is present in an amount at least equal to or greater than 10 wt%.
- homogeneous blends of SRC (above 40 wt%) and second-stage process solvent can be effected only if first-stage process solvent is present in amounts of at least 20 wt%.
- Deashed SRC is a product derived from the first and/or second stage liquefaction of solvent refined coal (SRC-I) and it can be dissolved with SRC distillate oils in pulverized (solid) form or in molten form.
- SRC A first-stage solvent-refined coal product (nominally greater than 850° F.) obtained after a deashing process.
- HSRC Heavy SRC; a first-stage solvent-refined coal product recovered from the SRC-I process after critical solvent deashing.
- TSL SRC A product obtained via the two-stage liquefaction of SRC (i.e., hydrocracked SRC).
- Middle Oil 400°-650° F. (first and second stage oil)
- Heavy Oil 650°-850° F. (first and second stage oil)
- the SRC solids of this invention may be dissolved in coal liquid distillates in solid form or liquid form. They are prepared by first forming an SRC mineral ash slurry and subjecting the mixture to a separation procedure, optionally followed by a hydrocracking step. This procedure is described in detail below.
- SRC Mineral Ash Slurry Dry pulverized coal slurried with process solvent was pumped to reaction pressure. The slurry was heated against hot process solvent in coal exchangers, hot hydrogen-rich recycle gas was added to the pressurized slurry and the mixture was heated to reaction temperature. There was thus obtained a slurry containing low-sulphur solvent-refined coal (SRC) and mineral ash residue with distillate liquid and gaseous by-products.
- SRC low-sulphur solvent-refined coal
- distillate liquid by-products were separated into medium and heavy oil fractions for the recovery of process solvent and unreacted hydrogen was recovered, purified and recycled to the coal exchanger for re-use in the preparation of additional slurry.
- Deashed Molten SRC The SRC mineral ash slurry of the previous step was mixed with proprietary solvent and pumped to a first-stage settler in which a heavy phase and a light phase separated. The light phase was passed into a second stage settler where a heavy phase and light phase again separated.
- the light phase from the second stage settler was passed into a third stage settler where light SRC was separated from the mixture and critical solvent was removed from the remaining heavy phase to afford deashed molten SRC.
- Deashed SRC Solids Deashed molten SRC from the prior step can be divided into three streams. One stream was sent to a hydrocracker for liquid distillate production, another was passed into a coker-calciner for coke production and the remaining stream was sent to a molten SRC tank where SRC was cooled and solidified.
- the SRC solids are pulverized according to the following procedures depending upon whether a small scale (laboratory) or large scale (pilot-plant) preparation of residual oil blends is desired.
- Molten SRC Blends Molten TSL SRC (200 lbs) maintained at about 600° F. was passed at a flow-rate of approximately 100 lbs per/hr into a 55 gallon closed head drum containing 200 lbs of a 1:1 mixture of first and second-stage process solvents at ambient temperature. The resulting mixture reached a maximum temperature of 350° F. and upon cooling there was obtained an SRC single-phase residual oil blend which exhibited the viscosity characteristics of a homogeneous mixture.
- the second stage middle oil and first stage heavy oil contain a preponderance of heavy components and, as a result, they are more viscous than their respective first-stage middle oil and second-stage heavy oil counter parts.
- Tables 6 and 7 show the relationship between temperature and viscosity for the first and second stage middle and heavy oils. The liquids exhibited Newtonian behavior over all temperature ranges:
- HSRC and TSL SRC solids were pulverized to a fineness of 100% through 140 mesh, approximately 105 ⁇ m.
- Single-phase blends were prepared in a three-necked, round-bottomed flask (500 ml) equipped with a thermometer and a glass stirrer. Fifty percent by weight of pulverized solids were added to preheated distillate liquids with constant stirring as described below. To assure complete dissolution and homogeneous mixing, the solids were added slowly over a 4 hr period at the required blending temperature (i.e., 200 ⁇ 5° F. for HSRC and TSL SRC, respectively) maintained for at least 12 hours.
- the required blending temperature i.e. 200 ⁇ 5° F. for HSRC and TSL SRC, respectively
- HSRC forms homogeneous blends with first stage distillate oils at all concentration levels. This is attributable to the presence in HSRC of high concentrations of preasphaltenes, that is, pyridine solubles rich in highly polar functional groups. Accordingly, the complete solubilization of HSRC requires a solvent having a polarity equal to or greater than pyridine.
- First-stage distillate oils possess an essentially identical profile, that is, they are relatively high in heteroatom content and possess high polarity as a result of which they solubilize the highly polar HSRC.
- TSL SRC has a negligible concentration of preasphaltenes. Accordingly, it is compatible with the low heteroatom content of the second-stage oil and is solubilized thereby. See in this regard the reduced heteroatom content (polarity) of the second-stage distillate oil as compared to the first stage oil in Table 1.
- TSL SRC forms homogeneous blends with first-and second-stage distillate oils or mixtures of same at all concentration levels.
- Example 2 illustrates the limited solubility of HSRC in second-stage oils even when additions are made close to the flash point temperatures.
- the inability of the second-stage oils to completely solubilize HSRC is attributed to the low heteroatom content (i.e., low polarity) of the second-stage oil.
- Example 1 The procedure of Example 1 was repeated except that 50 wt% of pulverized HSRC was added to second-stage middle oil and second-stage heavy oil.
- HSRC pyridine-soluble preasphaltenes, that is, compounds rich in polar functional groups. Accordingly, the complete solubilization of HSRC requires the use of solvents having a polarity equal to or greater than that of pyridine. Unfortunately, the low heteroatom second-stage oils do not possess this property.
- Example 1 The procedure of Example 1 was repeated except that HSRC was combined with mixtures of first-stage heavy oil and second-stage heavy oil.
- Table 16 lists the viscosities observed for a blend of 40 wt% HSRC solids with 10 wt% first-stage heavy oil and 50 wt% second-stage heavy oil over a range of temperatures and shear rates:
- Table 17 lists the viscosities observed for a blend of 50 wt% HSRC solids with 10 wt% first-stage heavy oil and 40 wt% second-stage heavy oil over a range of temperatures and shear rates:
- first-stage oil is necessary to solubilize the HSRC solids because the low-heteroatom content of the second-stage oils is not sufficient to solubilize HSRC.
- first-stage oils are rich in heteroatom content and their addition to second-stage oil results in an increase in polarity to the extent that it solubilizes HSRC.
- Table 18 lists the viscosities for a blend of HSRC with second-stage middle oil and first-stage heavy oil over a range of temperatures and shear rates:
- first-stage heavy oil due to the small heteroatom content of second-stage middle oil relatively high concentrations of first-stage heavy oil (rich in heteroatom content) are needed to prepare single-phase HSRC blends.
- the data in Table 18 indicates that first-stage oil concentrations in excess of 15 wt% should be added to HSRC and second-stage middle oil in order to prepare a 40 wt% HSRC single-phase blend in second-stage middle oil.
- the blend in Table 18 developed a partial separation of a oil phase at ambient temperature. Moreover, the decrease in viscosity and concomitant increase in shear rate is indicative of multi-phase mixture rather than a homogeneous blend.
- Blends containing more than 40 wt% of HSRC and second-stage process solvent require the addition of first-stage process solvent in amounts at least equal to 20 wt% in order to afford homogeneous fuel oil blends.
- Table 19 summarizes the viscosity/temperature data for the single-phase blend of 50 wt% HSRC in a 2:3 mixture of first-and second-stage process solvents.
- the foregoing data supports the view that the rich heteroatom content of the first-stage process solvent is required in amounts of at least 20 wt% in order to fully solubilize the HSRC solids.
- HSRC and TSL SRC blend compositions simulate, respectively, the first-stage and second-stage SRC-I Demonstration Plant total blended products (excluding naphtha and anode coke).
- Table 20 shows that the H/C ratio and heating values increase in the following order: HSRC blend ⁇ TSL SRC blend ⁇ No. 6 Fuel Oil.
- the residual oils were then subjected to a 4-5 month storage stability test at 150° F. in controlled nitrogen and air atmospheres.
- Various 1 oz. vials each containing approximately 10 ml of the residual oil, were capped after flushing with the desired gas and then stored in a 150° F. isothermal oven. The temperature and atmosphere of the oven were maintained by the slow circulation of the gas.
- one vial of each residual oil was taken from the oven to measure viscosities at three temperatures used to monitor fuel aging with time.
- FIGS. 2-4 depict the resulting changes in viscosity.
- FIG. 5 shows that the temperature increases required to bring 140-day air- and nitrogen-aged HSRC residual-oil samples to the original pumping viscosity of 1,000 cP were 10° and 6° F., respectively.
- FIG. 6 shows that the temperature increases required to bring the 120-day air- and nitrogen-aged No. 6 Fuel Oil samples to the original pumping viscosity of 1,000 cP were 8° and 4° F., respectively.
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Abstract
Coal solids (SRC) and distillate oils are combined to afford single-phase blends of residual oils which have utility as fuel oils substitutes. The components are combined on the basis of their respective polarities, that is, on the basis of their heteroatom content, to assure complete solubilization of SRC. The resulting composition is a fuel oil blend which retains its stability and homogeneity over the long term.
Description
The Government of the United States of America has rights in this invention pursuant to Contract No. DE-AC05780RO3054 (as modified) awarded by the U.S. Department of Energy.
This invention relates to a composition of matter which has utility as a fuel oil substitute.
More specifically, this invention relates to a blend of solvent refined coal in a mixture of distillate oils. The resulting composition exhibits long term stability as a fuel oil and it may be used with only minor modification in existing infrastructures.
Coal refining consists of adding hydrogen to coal and removing its principal pollutants, sulphur and ash. First, raw coal is pulverized, mixed with a solvent derived from the refining process and heated under pressure. Hydrogen is added and the hydrogenated coal-solvent mixture is sent to a reactor vessel where liquefaction occurs. The resulting mixture is passed to a separator, naphtha and distillate liquids are drawn off, sulphur is removed as hydrogen sulphide and ash is eliminated by a conventional deashing step.
The principal product of this operation is solvent refined coal, that is, SRC which at ambient temperature is a shiny, black solid. Upon subjecting SRC to hydrogenation in a catalytic hydrocracker there is also produced TSL SRC a solid residual fuel having very low sulphur content and more naphtha and distillate liquids.
Compositions comprised of solvent refined coal and distillate oils have been reported in the literature but their use as fuel oil substitutes has not been widely accepted due to their instability over the long term. It has heretofore been believed that the asphaltenes and preasphaltenes content of the SRC would always result in an unstable mixture of SRC and coal derived liquids.
In Annual Reports by the Electric Power Research Institute (EPRI) entitled "Upgrading of Coal Liquids For Use as Power Generation Fuels," published October, 1977, December 1978, and December 1979 as Reports AF444, AF873 and AF1255 there are described blends of SRC fuel in recycled solvents. With these blends complete solubilization was not achieved due to the presence of two phases at temperatures up to 300° F. and/or benzene insoluble compounds which separated from solution over extended periods attributed to oxidation and degradation at high SRC concentrations.
In an article captioned "Viscosity of Coal Liquids--The Effect of Character and Content of the Non-Distillable Portion" (Journal of the American Chemical Society, Division of Fuel Chemistry, Volume 22: pages 33-48; 1977) J. Schiller describes a simulated fuel oil comprised of finely ground distillation residues derived from SRC and anthracene oils. These compositions exhibit a low viscosity which Schiller attributes to the synergistic effect of asphaltene on anthracene oil.
Asphaltenes are polar compounds which are found in distillation residues. They are high in heteroatom content and they possess hydroxy and nitrogen moieties which contribute to the formation of insoluble residues; however, Schiller observed, surprisingly, that the synergistic effect of asphaltene resulted in a composition free of undissolved solids. Unfortunately, however, the distillation residues in these liquids do not remain in solution indefinitely and, therefore, the synergistic effect of asphaltene cannot explain fully the undissolved solids which have been observed over extended storage periods.
FIGS. 1-6 graphically depict the viscosity characteristics of solvent refined coal-distillate oil blends as well as the viscosity characteristics of No. 6 fuel oil in relation to temperature and storage time.
It has been discovered that deashed solvent refined coal (SRC or TSL SRC) can be combined with the distillate oils of solvent refined coal to provide compositions which are uniquely stable over long periods, a feature which makes them suitable as simulated fuel oils. The term `SRC` is used herein to jointly and severally refer to the various sources of non-distillate solvent-refined coal products, nominally, 850° F.+ coal, for example, SRC, HSRC and TSL SRC.
Accordingly, it is an object of this invention to describe novel blends of SRC and SRC distillate oils which can be used as a No. 6 fuel oil substitute and which remain homogeneous in a single phase over extended periods.
It is a further object to describe novel means for producing single-phase homogeneous blends of SRC and SRC distillate oils by utilizing parameters which make it possible to customize the blend to specification.
A unique feature of this invention lies in the discovery that a correlation exists between the homogeneity of SRC fuel oil and the heteroatom composition of the distillate oils and the particular SRC which are mixed.
The evaluation of residual SRC oils as fuel oil substitutes led to the discovery that homogeneity and stability depend to a large extent on component characterization. SRC solids, for example, are rich in nitrogen, oxygen and sulphur, that is, heteroatoms which exert a high degree of polarity within the molecule. A contributor to this effect are the preasphaltenes which are present in solvent refined coal in appreciable amounts. The preasphaltenes are pyridine solubles rich in polar functional groups and it has been found that solubilization of SRC requires solvents having a polarity at least equal to or greater than pyridine.
This invention provides guidelines for optimizing the solubility of SRC solids in distillate oils. It identifies the polarity requirement of the solvent necessary to form homogeneous residual oil blends and specifies the compositions of heteroatom rich first-stage oil to be added to make SRC and second-stage oil homogeneous blends.
More specifically, this invention relates to a homogeneous, single-phase blend of fuel oil consisting essentially of deashed solvent-refined coal and distillate oils derived from the liquefaction of coal, said oils having a heteroatom content greater than about 25 wt% of the heteroatom content of said solvent-refined coal.
The distillate oils employed in this invention are first- and second-stage distillate oils having a boiling range of 400°-1000° F.; they are comprised nominally of 400°-650° F. middle oil, 650°-850° F. heavy oil and 450°-850° F. process solvent. These distillate oils can be used individually or they can be used in various combinations with deashed SRC to provide a homogeneous single-phase SRC residual oil blend having viscosity-temperature characteristics which make it suitable for use of substitute for No. 6 fuel oil.
The amount of distillate oil combined with deashed solvent-refined coal depends upon the heteroatom content of the distillate oil employed. At concentrations equal to or greater than 40 wt% deashed solvent refined coal cannot be mixed even at temperatures close to its flash point to form homogeneous blends with middle oil, heavy oil or process solvent of the second stage.
Generally, first stage distillate oils contain the greatest concentration of heteroatoms and, therefore, deashed solvent-refined coal (SRC) forms homogeneous blends with first-stage distillate oils at all concentrations.
On the other hand, homogeneous blends of SRC (above 40 wt%) and second-stage middle oil require the addition of first-stage heavy oil in quantities greater than 15 wt%. According to another embodiment a homogeneous blend of SRC and second-stage heavy oil can be made only if first-stage heavy oil is present in an amount at least equal to or greater than 10 wt%.
Accordng to still another embodiment homogeneous blends of SRC (above 40 wt%) and second-stage process solvent can be effected only if first-stage process solvent is present in amounts of at least 20 wt%.
Deashed SRC is a product derived from the first and/or second stage liquefaction of solvent refined coal (SRC-I) and it can be dissolved with SRC distillate oils in pulverized (solid) form or in molten form.
The following is a list of SRC solids and distillate oils referred to in this application.
SRC: A first-stage solvent-refined coal product (nominally greater than 850° F.) obtained after a deashing process.
HSRC: Heavy SRC; a first-stage solvent-refined coal product recovered from the SRC-I process after critical solvent deashing.
TSL SRC: A product obtained via the two-stage liquefaction of SRC (i.e., hydrocracked SRC).
Note: The term "SRC" is often used as an abbreviation for all solvent-refined coal non-distillate products such as one or all three of the above as well as the first-stage product only.
Middle Oil: 400°-650° F. (first and second stage oil)
Heavy Oil: 650°-850° F. (first and second stage oil)
Process Solvent: 450°-850° F. (first & second stage oil)
The SRC solids of this invention may be dissolved in coal liquid distillates in solid form or liquid form. They are prepared by first forming an SRC mineral ash slurry and subjecting the mixture to a separation procedure, optionally followed by a hydrocracking step. This procedure is described in detail below.
SRC Mineral Ash Slurry: Dry pulverized coal slurried with process solvent was pumped to reaction pressure. The slurry was heated against hot process solvent in coal exchangers, hot hydrogen-rich recycle gas was added to the pressurized slurry and the mixture was heated to reaction temperature. There was thus obtained a slurry containing low-sulphur solvent-refined coal (SRC) and mineral ash residue with distillate liquid and gaseous by-products.
The distillate liquid by-products were separated into medium and heavy oil fractions for the recovery of process solvent and unreacted hydrogen was recovered, purified and recycled to the coal exchanger for re-use in the preparation of additional slurry.
Deashed Molten SRC: The SRC mineral ash slurry of the previous step was mixed with proprietary solvent and pumped to a first-stage settler in which a heavy phase and a light phase separated. The light phase was passed into a second stage settler where a heavy phase and light phase again separated.
The light phase from the second stage settler was passed into a third stage settler where light SRC was separated from the mixture and critical solvent was removed from the remaining heavy phase to afford deashed molten SRC.
Deashed SRC Solids: Deashed molten SRC from the prior step can be divided into three streams. One stream was sent to a hydrocracker for liquid distillate production, another was passed into a coker-calciner for coke production and the remaining stream was sent to a molten SRC tank where SRC was cooled and solidified.
The SRC solids are pulverized according to the following procedures depending upon whether a small scale (laboratory) or large scale (pilot-plant) preparation of residual oil blends is desired.
Small Scale Blends of SRC Solids: Deashed SRC solids were pulverized 100% to 140 mesh (approximately 105 μm) and this material was added with stirring to preheated distillate oil in a three-necked round-bottomed flash (500 ml) equipped with a thermometer. The solid was added slowly over a 4 hour period at the required blending temperature (i.e., 200±5° F. for SRC and 150±5° F. for TSL SRC) to assure complete dissolution and homogeneity and stirring was continued for an additional 12 hours.
Large Scale Blends of SRC Solids: Deashed SRC solids were pulverized to -200 mesh were quckly added through a closed solids feed port to distillate oil which had been preheated to 150°-220° F. in a closed steam-heated vessel equipped with a reflux condenser. The mixing step was effected using a low shear circulating pump and a nitrogen atmosphere was maintained in the vessel to prevent contact between the blended flue and ambient air. A homogeneous blend was obtained within about 45-60 minutes following the addition of SRC solids.
Molten SRC Blends: Molten TSL SRC (200 lbs) maintained at about 600° F. was passed at a flow-rate of approximately 100 lbs per/hr into a 55 gallon closed head drum containing 200 lbs of a 1:1 mixture of first and second-stage process solvents at ambient temperature. The resulting mixture reached a maximum temperature of 350° F. and upon cooling there was obtained an SRC single-phase residual oil blend which exhibited the viscosity characteristics of a homogeneous mixture.
The following examples illustrate the effect of heteroatom concentration on SRC solubility. All first- and second-stage solids and all distillate oils employed in these studies exhibited the following heteroatom content:
TABLE 1
______________________________________
Properties of Fuel Oil Blend Components
1st-Stage 2nd-Stage
Mid- Mid-
dle Heavy dle Heavy
Component:
HSRC Oil Oil TSL SRC Oil Oil
______________________________________
Ultimate
analysis
(wt %)
C 85.86 86.24 86.89 89.95 88.89
89.40
H 6.03 8.98 7.81 6.98 10.28
9.11
N 1.78 0.60 1.25 1.34 0.39
0.85
O 5.15 3.93 3.28 1.56 0.44
0.61
S 1.08 0.25 0.77 0.17 0.00
0.03
Ash 0.10 -- -- -- --
H/C, atomic
0.843 1.249 1.079 0.931 1.388
1.223
ratio
______________________________________
This data shows that the first stage components and lower H/C ratios and a higher heteroatom content than their second-stage counterparts. The boiling point distribution for the distillate oils of Table 1, determined by the standard ASTM D2887 simulated distillation method, is given in Tables 2-5:
TABLE 2
______________________________________
Boiling Point Distribution of 1st-Stage
Middle Oil by ASTM 02887
% Dist. Temp. (°F.)
% Dist. Temp. (°F.)
______________________________________
IBP 391 60 540
5 416 70 574
10 424 80 607
20 438 90 641
30 462 95 664
40 486 99 729
50 516 FBP 783
______________________________________
TABLE 3
______________________________________
Boiling Point Distribution of 1st-Stage
Heavy Oil by ASTM D2887
% Dist. Temp. (°F.)
% Dist. Temp. (°F.)
______________________________________
IBP 660 60 781
5 682 70 806
10 692 80 841
20 710 90 899
30 726 95 952
40 743 99 1010
50 761 FBP 1027
______________________________________
TABLE 4
______________________________________
Boiling Point Distribution of 2nd-Stage
Middle Oil by ASTM D2887
% Dist. Temp. (°F.)
% Dist. Temp. (°F.)
______________________________________
IBP 375 60 587
5 422 70 606
10 450 80 626
20 489 90 647
30 520 95 658
40 541 99 681
50 562 FBP 708
______________________________________
TABLE 5
______________________________________
Boiling Point Distribution of 2nd-Stage
Heavy Oil by ASTM D2887
% Dist Temp. (°F.)
% Dist. Temp. (°F.)
______________________________________
IBP 640 60 759
5 663 70 783
10 674 80 813
20 691 90 862
30 705 95 906
40 722 99 1010
50 739 FBP 1035
______________________________________
The foregoing shows that the second stage middle oil and first stage heavy oil contain a preponderance of heavy components and, as a result, they are more viscous than their respective first-stage middle oil and second-stage heavy oil counter parts.
Tables 6 and 7 show the relationship between temperature and viscosity for the first and second stage middle and heavy oils. The liquids exhibited Newtonian behavior over all temperature ranges:
TABLE 6
______________________________________
Variation of Viscosity with Temperature,
1st-Stage Middle and Heavy Oils
Temperature Shear Rate
Viscosity
Oil (°F.) (sec.sup.-1)
(cP)
______________________________________
Middle 70 79.20 9.6
39.60 9.6
80 79.20 7.2
39.60 7.0
90 79.20 4.8
39.60 4.7
Heavy 100 2.04 8288
1.02 8292
0.51 8300
110 4.08 3019
2.04 3021
1.02 3025
120 10.20 1343
4.08 1350
2.04 1350
125 20.40 925
10.20 935
4.08 938
135 20.40 500
10.20 500
4.08 500
145 15.84 274
7.92 273
3.96 275
155 39.60 163
15.84 164
7.92 164
165 79.20 103
30.60 104
15.84 104
180 79.20 57.9
39.60 58.0
15.84 57.9
200 79.20 30.4
39.60 30.5
______________________________________
TABLE 7
______________________________________
Variation of Viscosity with Temperature,
2nd-Stage Middle and Heavy Oils
Temperature Shear Rate
Viscosity
Oil (°F.) (sec.sup.-1)
(cP)
______________________________________
Middle 70 79.20 10.6
39.60 10.7
80 79.20 7.7
39.60 7.6
90 79.20 5.9
39.60 5.9
Heavy 74 1.98 2915
0.79 2917
80 3.96 1715
1.98 1730
0.79 1738
85 7.92 1178
3.96 1180
1.98 1185
90 7.92 829
3.96 833
1.98 835
95 15.84 584
7.92 591
3.96 593
100 15.84 441
7.92 444
3.96 443
110 15.84 256
7.92 258
3.96 260
120 39.60 152
15.84 154
7.92 155
140 79.20 66.8
39.60 66.8
15.84 66.9
165 79.20 29.9
39.60 30.0
15.84 30.0
______________________________________
The data of Tables 6 and 7 show that the viscosity of the liquid is related to its structural composition and heteroatom content.
This invention will now be illustrated by reference to specific embodiments.
HSRC and TSL SRC solids were pulverized to a fineness of 100% through 140 mesh, approximately 105 μm. Single-phase blends were prepared in a three-necked, round-bottomed flask (500 ml) equipped with a thermometer and a glass stirrer. Fifty percent by weight of pulverized solids were added to preheated distillate liquids with constant stirring as described below. To assure complete dissolution and homogeneous mixing, the solids were added slowly over a 4 hr period at the required blending temperature (i.e., 200±5° F. for HSRC and TSL SRC, respectively) maintained for at least 12 hours.
The following blends of 50 wt% solid composition were prepared:
HSRC/1st-stage middle oil
HSRC/1st stage heavy oil
TSL SRC/1st-stage middle oil
TSL SRC/2nd stage middle oil
TSL SRC/1st-stage heavy oil
TSL SRC/2nd-stage heavy oil
The viscosities of the blends at specific temperatures and shear rates, as determined by a Brookfield viscometer, are listed in Tables 8-13. The range of applied shear rates varied with the viscosity of the blend and the spindle used. The blends behaved like a Newtonian liquid within experimental error. All blends were solid at ambient temperature and showed no separation of a liquid phase.
TABLE 8
______________________________________
Variation of Viscosity with Temperature,
50 wt % HSRC in 1st-Stage Middle Oil
Temperature Shear Rate
Viscosity
(°F.) (sec.sup.-1)
(cP)
______________________________________
100 0.20 68,500
0.10 69,000
115 1.02 16,600
0.51 16,800
0.20 17,000
130 4.08 5,125
2.04 5,175
1.02 5,200
145 10.20 1,938
4.08 1,956
2.04 1,963
160 20.40 859
10.20 868
4.08 869
175 15.84 382
7.92 385
3.96 388
190 39.60 200
15.84 201
7.92 204
215 79.20 82.1
39.60 83.0
15.84 83.1
240 79.20 41.5
39.60 41.3
15.84 41.9
265 79.20 22.6
39.60 23.0
______________________________________
TABLE 9
______________________________________
Variation of Viscosity with Temperature,
50 wt % HSRC in 1st-Stage Heavy Oil
Temperature Shear Rate
Viscosity
(°F.) (sec.sup.-1)
(cP)
______________________________________
220 0.84 31,350
0.42 31,533
0.17 31,750
230 1.68 14,950
0.84 14,950
0.42 15,000
240 3.36 7,450
1.68 7,467
0.84 7,467
250 1.98 3,700
0.79 3,725
0.40 3,750
270 7.92 1,201
3.96 1,213
1.98 1,220
290 15.84 463
7.92 464
3.96 468
310 39.60 209
15.84 211
7.92 214
335 79.20 95.0
39.60 95.0
15.84 96.3
360 79.20 48.4
39.60 48.3
385 79.20 27.9
39.60 28.3
415 79.20 16.1
39.60 16.0
______________________________________
TABLE 10
______________________________________
Variation of Viscosity with Temperature,
50 wt % TSL SRC in 1st-Stage Middle Oil
Temperature Shear Rate
Viscosity
(°F.) (sec.sup.-1)
(cP)
______________________________________
75 2.04 6,738
1.02 6,775
0.51 6,900
85 4.08 3,300
2.04 3,325
1.02 3,350
95 10.20 1,683
4.08 1,700
2.04 1,725
105 20.40 931
10.20 943
4.08 956
120 15.84 423
7.92 428
3.96 433
135 39.60 212
15.84 215
7.92 219
155 79.20 99.1
39.60 100
15.84 102
180 79.20 47.6
39.60 47.5
15.84 48.8
200 79.20 28.8
39.60 29.3
15.84 30.6
225 79.20 17.4
39.60 18.0
______________________________________
TABLE 11
______________________________________
Variation of Viscosity with Temperature,
50 wt % TSL SRC in 2nd-Stage Middle Oil
Temperature Shear Rate
Viscosity
(°F.) (sec.sup.-1)
(cP)
______________________________________
75 2.04 11,188
1.02 11,300
0.51 11,350
85 4.08 5,231
2.04 5,300
1.02 5,300
95 4.08 2,694
2.04 2,700
1.02 2,700
105 10.20 1,465
4.08 1,469
2.04 1,471
120 15.84 607
7.92 615
3.96 618
135 15.84 305
7.92 306
3.96 308
155 39.60 137
15.84 137
7.92 138
180 79.20 60.3
39.60 60.8
15.84 61.3
200 79.20 35.8
39.60 35.8
225 79.20 20.6
39.60 20.8
______________________________________
TABLE 12
______________________________________
Variation of Viscosity with Temperature,
50 wt % TSL SRC in 1st-Stage Heavy Oil
Temperature Shear Rate
Viscosity
(°F.) (sec.sup.-1)
(cP)
______________________________________
170 0.20 58,125
0.10 58,500
185 1.02 15,825
0.51 15,850
0.20 15,875
200 4.08 5,200
2.04 5,225
1.02 5,225
215 10.20 1,980
4.08 1,981
2.04 1,988
230 20.40 861
10.20 861
4.08 863
245 15.84 408
7.92 409
3.96 410
260 39.60 221
15.84 221
7.92 221
275 39.60 129
15.84 129
7.92 129
295 79.20 69.0
39.60 69.4
315 79.20 40.6
39.60 40.6
340 79.20 23.4
39.60 23.3
365 79.20 14.6
39.60 14.5
______________________________________
TABLE 13
______________________________________
Variation of Viscosity with Temperature,
50 wt % TSL SRC in 2nd-Stage Heavy Oil
Temperature Shear Rate
Viscosity
(°F.) (sec.sup.-1)
(cP)
______________________________________
150 0.20 56,750
0.10 56,750
170 2.04 11,100
1.02 11,125
0.51 11,150
190 4.08 2,994
2.04 3,000
1.02 3,000
210 20.40 973
10.20 978
4.08 975
220 20.40 601
10.20 603
4.08 606
240 39.60 247
15.84 248
7.92 250
265 79.20 106
39.60 106
15.84 105
290 79.20 52.5
39.60 52.5
310 79.20 32.4
39.60 32.3
330 79.20 17.9
39.60 17.9
______________________________________
The foregoing shows that HSRC forms homogeneous blends with first stage distillate oils at all concentration levels. This is attributable to the presence in HSRC of high concentrations of preasphaltenes, that is, pyridine solubles rich in highly polar functional groups. Accordingly, the complete solubilization of HSRC requires a solvent having a polarity equal to or greater than pyridine. First-stage distillate oils possess an essentially identical profile, that is, they are relatively high in heteroatom content and possess high polarity as a result of which they solubilize the highly polar HSRC.
On the other hand, second-stage distillate oils are not sufficiently rich in heteroatom content and their low polarity make it impossible to solubilize HSRC. This conclusion is supported by the observations reported in Example 2 and the accompanying Tables 14 and 15.
By contrast, TSL SRC has a negligible concentration of preasphaltenes. Accordingly, it is compatible with the low heteroatom content of the second-stage oil and is solubilized thereby. See in this regard the reduced heteroatom content (polarity) of the second-stage distillate oil as compared to the first stage oil in Table 1.
Indeed, TSL SRC forms homogeneous blends with first-and second-stage distillate oils or mixtures of same at all concentration levels.
Example 2 illustrates the limited solubility of HSRC in second-stage oils even when additions are made close to the flash point temperatures. The inability of the second-stage oils to completely solubilize HSRC is attributed to the low heteroatom content (i.e., low polarity) of the second-stage oil.
The procedure of Example 1 was repeated except that 50 wt% of pulverized HSRC was added to second-stage middle oil and second-stage heavy oil.
A partial separation of the oil phase in both preparations was observed at ambient temperature.
The variation in viscosity and shear rates over a range of temperatures are listed in Tables 14 and 15.
TABLE 14
______________________________________
Variation of Viscosity with Temperature,
50 wt % HSRC in 2nd-Stage Middle Oil
Temperature Shear Rate
Viscosity
(°F.) (sec.sup.-1)
(cP)
______________________________________
115 0.79 8,125
0.40 12,100
130 1.98 2,170
0.79 3,925
0.40 6,242
145 7.92 788
3.96 1,043
1.98 1,257
160 15.84 372
7.92 496
3.96 719
175 39.60 228
15.84 281
7.92 405
250 79.20 67
39.60 102
15.84 216
______________________________________
TABLE 15
______________________________________
Variation of Viscosity with Temperature,
50 wt % HSRC in 2nd-Stage Heavy Oil
Temperature Shear Rate
Viscosity
(°F.) (sec.sup.-1)
(cP)
______________________________________
240 0.20 9,738
0.10 16,150
265 20.40 686
10.20 1,217
4.08 2,569
290 20.40 529
10.20 1,018
4.08 1,738
315 20.4 341
10.20 425
______________________________________
The observed decrease in viscosity with shear rates is indicative of a multi-phase composition rather than a homogeneous blend of components.
Moreover, the observed viscosities in second-stage middle oil (Table 14) and the viscosities observed in second-stage heavy oil (Table 15) indicate that at the specified temperatures the viscosity of each mixture depended on the applied shear rate. The non-Newtonian behavior of these mixtures suggests that the blends do not exist as single phase compositions due to the limited solubility of HSRC in second-stage oils. Partial separation of the oil phase was also observed when mixtures were allowed to cool to ambient temperature, further substantiating the non-homogeneous nature of these mixtures.
A major portion of HSRC consists of pyridine-soluble preasphaltenes, that is, compounds rich in polar functional groups. Accordingly, the complete solubilization of HSRC requires the use of solvents having a polarity equal to or greater than that of pyridine. Unfortunately, the low heteroatom second-stage oils do not possess this property.
The procedure of Example 1 was repeated except that HSRC was combined with mixtures of first-stage heavy oil and second-stage heavy oil.
Table 16 lists the viscosities observed for a blend of 40 wt% HSRC solids with 10 wt% first-stage heavy oil and 50 wt% second-stage heavy oil over a range of temperatures and shear rates:
TABLE 16
______________________________________
Variation of Viscosity with Temperature,
(HSRC - 40 wt %, Heavy Oil 1st-Stage - 10 wt %,
Heavy Oil 2nd-Stage - 50 wt %)
Temperature Shear Rate
Viscosity
(°F.) (sec.sup.-1)
(cP)
______________________________________
180 0.20 54,750
0.10 54,750
200 2.04 7,350
1.02 7,350
0.51 7,400
220 10.20 1,755
4.08 1,763
2.04 1,775
230 20.40 1,055
10.20 1,066
4.08 1,069
240 20.40 628
10.20 628
4.08 631
260 39.60 238
15.84 239
7.92 240
280 79.20 110
39.60 110
15.84 113
305 79.20 50.9
39.60 51.0
330 79.20 27.4
39.60 28.0
______________________________________
Table 17 lists the viscosities observed for a blend of 50 wt% HSRC solids with 10 wt% first-stage heavy oil and 40 wt% second-stage heavy oil over a range of temperatures and shear rates:
TABLE 17
______________________________________
Variation of Viscosity with Temperature,
(HSRC - 50 wt %, Heavy Oil 1st-Stage - 10 wt %,
Heavy Oil 2nd-Stage - 40 wt %)
Temperature Shear Rate
Viscosity
(°F.) (sec.sup.-1 1)
(cP)
______________________________________
220 0.20 52,500
0.10 53,250
240 2.04 9,188
1.02 9,175
0.51 9,200
255 4.08 3,100
2.04 3,125
1.02 3,125
265 10.20 1,685
4.08 1,688
2.04 1,688
275 20.40 980
10.20 983
4.08 988
295 20.40 379
10.20 380
315 39.60 165
15.84 167
7.92 168
335 79.20 87.5
39.60 87.5
360 79.20 45.1
39.60 45.2
390 79.20 23.4
39.60 23.4
______________________________________
Both HSRC mixtures provided single-phase homogeneous blends. These observations and the supporting data support the view that a homogeneous blend of HSRC and second-stage heavy oil can be made if first-stage heavy oil is added in amounts at least equal to or greater than 10 wt%.
The addition of first-stage oil is necessary to solubilize the HSRC solids because the low-heteroatom content of the second-stage oils is not sufficient to solubilize HSRC. By contrast, the first-stage oils are rich in heteroatom content and their addition to second-stage oil results in an increase in polarity to the extent that it solubilizes HSRC.
By following the procedure of Example 1 using HSRC, second-stage middle oil and first-stage heavy oil in various combinations, it was determined that homogeneous blends of HSRC and second-stage middle oil require the addition of first-stage heavy oil in amounts greater than 15 wt%.
Table 18 lists the viscosities for a blend of HSRC with second-stage middle oil and first-stage heavy oil over a range of temperatures and shear rates:
TABLE 18
______________________________________
Variation of Viscosity with Temperature,
(HSRC - 40 wt %, Heavy Oil 1st-Stage - 15 wt %,
Middle Oil 2nd-Stage - 45 wt %)
Temperature Shear Rate
Viscosity
(°F.) (sec.sup.-1)
(cP)
______________________________________
120 10.20 2,155
4.08 2,775
2.04 3,738
150 20.40 843
10.20 898
4.08 1,181
180 20.40 329
10.20 345
______________________________________
Due to the small heteroatom content of second-stage middle oil relatively high concentrations of first-stage heavy oil (rich in heteroatom content) are needed to prepare single-phase HSRC blends. The data in Table 18 indicates that first-stage oil concentrations in excess of 15 wt% should be added to HSRC and second-stage middle oil in order to prepare a 40 wt% HSRC single-phase blend in second-stage middle oil.
The blend in Table 18 developed a partial separation of a oil phase at ambient temperature. Moreover, the decrease in viscosity and concomitant increase in shear rate is indicative of multi-phase mixture rather than a homogeneous blend.
Blends containing more than 40 wt% of HSRC and second-stage process solvent require the addition of first-stage process solvent in amounts at least equal to 20 wt% in order to afford homogeneous fuel oil blends.
Table 19 summarizes the viscosity/temperature data for the single-phase blend of 50 wt% HSRC in a 2:3 mixture of first-and second-stage process solvents.
TABLE 19
______________________________________
Variation of Viscosity with Temperature,
HSRC: 50 wt %, Process Solvent 1st-Stage: 20 wt %,
Process Solvent 2nd-Stage: 30 wt %
Temperature Shear Rate
Viscosity
(°F.) (sec.sup.-1)
(cP)
______________________________________
169 4.08 5056
2.04 5113
1.02 5125
179 4.08 2500
2.04 2525
1.02 2550
189 10.20 1345
4.08 1356
2.04 1363
194 20.40 1005
10.20 1015
4.08 1019
204 20.40 616
10.20 620
219 15.84 294
7.92 294
3.96 300
240 39.60 133
15.84 132
7.92 133
260 79.20 69.0
39.60 69.0
15.84 69.4
286 79.20 35.4
39.60 35.3
291 79.20 33.8
39.60 33.8
311 79.20 23.8
39.60 23.8
______________________________________
The foregoing data supports the view that the rich heteroatom content of the first-stage process solvent is required in amounts of at least 20 wt% in order to fully solubilize the HSRC solids.
The following residual fuel oils were subjected to storage stability testing:
______________________________________
Fuel composition (wt %)
Component # 1 #2 #3
______________________________________
HSRC 50 -- --
1st-stage middle oil
40 30 --
1st-stage heavy oil
10 5 --
TSL SRC -- 50 --
2nd-stage middle oil
-- 12 --
2nd-stage heavy oil
-- 3 --
No. 6 Fuel Oil
-- -- 100
______________________________________
The above HSRC and TSL SRC blend compositions simulate, respectively, the first-stage and second-stage SRC-I Demonstration Plant total blended products (excluding naphtha and anode coke). Table 20 shows that the H/C ratio and heating values increase in the following order: HSRC blend <TSL SRC blend <No. 6 Fuel Oil.
TABLE 20
______________________________________
Properties of Residual Fuel Oils
Used for Stability Tests
No. 6
HSRC Blend TSL SRC Blend
Fuel Oil
Residual Oil
# 1 #2 #3
______________________________________
Ultimate Analysis, wt %
C 85.60 88.40 86.34
H 7.23 8.13 11.48
N 1.24 1.01 0.27
O 4.81 2.23 0.87
S 1.04 0.23 0.99
Ash 0.08 -- 0.05
H/C (atomic ratio)
1.014 1.104 1.596
Higher Heating
16.849 17.343 18.749
Value, Btu/lb
______________________________________
After 1 day there was sufficient evaporation of volatile components within the vapor space of the storage bottle as to require a 3° F. higher temperature to maintain the original viscosity. As shown in FIG. 1 the temperature required for the residual oils to reach viscosities of 30 cP (atomizing) and 1,000 cp (pumping) are as follows:
______________________________________
Temperature (°F.) at:
Residual Oil 30 cP 1,000 cP
______________________________________
HSRC blend (#1) 282 180
TSL SRC blend (#2)
217 121
No. 6 Fuel Oil (#3)
203 92
______________________________________
The residual oils were then subjected to a 4-5 month storage stability test at 150° F. in controlled nitrogen and air atmospheres. Various 1 oz. vials, each containing approximately 10 ml of the residual oil, were capped after flushing with the desired gas and then stored in a 150° F. isothermal oven. The temperature and atmosphere of the oven were maintained by the slow circulation of the gas. At specified intervals, one vial of each residual oil was taken from the oven to measure viscosities at three temperatures used to monitor fuel aging with time. FIGS. 2-4 depict the resulting changes in viscosity. Although the residual oils were stored in closed vials of the same size, some loss of volatiles undoubtedly occured during high-temperature storage, and such losses contribute to an increase in the viscosity. However, since storage conditions, temperatures, and viscosity measurement procedures were the same, the loss of material and its impact upon viscosity should be considered constant for the same residual oil stored under air or nitrogen. Therefore, it is apparent that storage in air had some adverse effect on the stability of No. 6 Fuel Oil and HSRC residual oil, but virtually no effect on TSL SRC residual oil.
The air-stored HSRC residual oil, the most rapid increase in viscosity occurred during the 20-60 day storage period; after 60 days, viscosity increased less rapidly. FIG. 5 shows that the temperature increases required to bring 140-day air- and nitrogen-aged HSRC residual-oil samples to the original pumping viscosity of 1,000 cP were 10° and 6° F., respectively. FIG. 6 shows that the temperature increases required to bring the 120-day air- and nitrogen-aged No. 6 Fuel Oil samples to the original pumping viscosity of 1,000 cP were 8° and 4° F., respectively. These results indicate that the storage stability of HSRC residual oils is comparable to that of No. 6 Fuel Oil, and the nitrogen blanketing during storage is important in maintaining the specified viscosity characteristics of the residual oils. An almost identical change in the viscosity of TSL SRC residual oil with storage time in nitrogen and air atmospheres suggests that such oils are relatively more stable than No. 6 Fuel Oil and HSRC residual oil, and that the viscosity increase during storage is mainly due to the loss of volatile components rather than to any associated aging effect.
Claims (8)
1. A homogeneous, single phase blend of fuel oil having long term viscosity stability consisting essentially of a blend of: (1) deashed solvent refined coal selected from the group consisting of a first-stage deashed 850° F.+ coal (SRC), a first-stage critical solvent deashed 850° F.+ coal (HSRC) and a two-stage liquefaction deashed 850° F.+ coal (TSL SRC) with (2) a distillate oil selected from the group consisting of a first-stage 400°-650° F. middle distillate oil, a first-stage 650°-850° F. heavy distillate oil, a first-stage 450°-850° F. coal liquefaction derived solvent, a second stage 400°-650° F. middle distillate oil, a second-stage 650°-850° F. heavy distillate oil, a second stage 450°-850° F. coal liquefaction process solvent and combinations thereof, wherein said selected solvent refined coal is present in said blend in a quantity of from 40 to 50 weight % based on the the weight of said blend and wherein said selected distillate oil or mixture thereof contains a heteroatom content of at least about 1/4 of the heteroatom content of said selected solvent refined coal.
2. The fuel oil of claim 1 wherein said solvent-refined coal is blended with said distillate oils in pulverized or molten form.
3. A fuel oil according to claim 1 wherein first-stage deashed 850° F.+ coal (SRC) is blended with a mixture of first-stage distillate oil and second-stage distillage oil.
4. A fuel oil according to claim 1 wherein first-stage deashed 850° F.+ coal (SRC) is blended with first-stage distillate oil.
5. A fuel oil according to claim 1 consisting essentially of first-stage deashed coal (SRC), second-stage heavy oil and first-stage heavy oil in an amount equal to or greater than 10 wt%.
6. A fuel oil according to claim 1 consisting essentially of first-stage deashed 850° F.+ coal (SRC), second-stage middle oil and first-stage heavy oil in an amount greater than 15 wt%.
7. A fuel oil according to claim 1 consistng essentially of first-stage deashed 850° F. coal (SRC), second-stage process solvent and first-stage process solvent in an amount at least equal to 20 wt%.
8. A method for preparing a homogeneous, single-phase blend of fuel oil which comprises blending two components, (1) a deashed solvent refined coal selected from the group consisting of a first-stage deashed 850° F.+ coal, a first-stage critical solvent deashed 850° F.+ coal and a two-stage liquefaction deashed 850° F.+ coal with (2) a distillate oil selected from the group consisting of a first-stage 400°-650° F. middle distillate oil, a first-stage 650°-850° F. heavy distillate oil, a first-stage 450°-850° F. coal liquefaction process solvent, a second-stage 400°-650° F. middle distillate oil, a second-stage 650°-850° F. heavy distillate oil, a second-stage 450°-850° F. coal liquefaction process solvent and combinations thereof, to the extent that the selected solvent refined coal is present in said blend in quantity of from 40 to 50 weight % based on the weight of said blend and wherein said selected distillate oil or mixture thereof contains a heteroatom content of at least about one quarter of the heteroatom content of said selected solvent refined coal.
Priority Applications (4)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US06/561,388 US4547201A (en) | 1983-12-14 | 1983-12-14 | SRC Residual fuel oils |
| CA000466392A CA1243204A (en) | 1983-12-14 | 1984-10-26 | Src residual fuel oils |
| AU34727/84A AU564513B2 (en) | 1983-12-14 | 1984-10-26 | Src residual fuel oils |
| ZA848593A ZA848593B (en) | 1983-12-14 | 1984-11-02 | Src residual fuel oils |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US06/561,388 US4547201A (en) | 1983-12-14 | 1983-12-14 | SRC Residual fuel oils |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| US4547201A true US4547201A (en) | 1985-10-15 |
Family
ID=24241736
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US06/561,388 Expired - Fee Related US4547201A (en) | 1983-12-14 | 1983-12-14 | SRC Residual fuel oils |
Country Status (4)
| Country | Link |
|---|---|
| US (1) | US4547201A (en) |
| AU (1) | AU564513B2 (en) |
| CA (1) | CA1243204A (en) |
| ZA (1) | ZA848593B (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4692270A (en) * | 1984-02-14 | 1987-09-08 | Nippon Petrochemicals Company, Limited | Surface active agent |
| US6435164B1 (en) * | 2000-12-07 | 2002-08-20 | Ford Global Technologies, Inc. | Fuel weathering method for vehicle evaporative emission system |
| US20110180266A1 (en) * | 2008-06-30 | 2011-07-28 | A.P. Meller-Mærsk A/S | Drill ship for deep sea intervention operations |
| US20180037831A1 (en) * | 2015-02-10 | 2018-02-08 | Avantium Knowledge Centre B.V. | Fuel composition comprising humins |
| CN109355083A (en) * | 2018-11-26 | 2019-02-19 | 中冶焦耐(大连)工程技术有限公司 | Process and system for extracting three-mixed fraction by tar reduced pressure distillation |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4133646A (en) * | 1976-10-18 | 1979-01-09 | Electric Power Research Institute, Inc. | Phenolic recycle solvent in two-stage coal liquefaction process |
| US4192653A (en) * | 1977-12-29 | 1980-03-11 | Gulf Research And Development Company | Novel fuel compositions comprising upgraded solid _and/or semi-solid material prepared from coal |
| US4203823A (en) * | 1978-07-03 | 1980-05-20 | Gulf Research & Development Company | Combined coal liquefaction-gasification process |
| US4276053A (en) * | 1978-12-13 | 1981-06-30 | The British Petroleum Company Limited | Fuel composition and method for its preparation |
| US4376032A (en) * | 1981-05-29 | 1983-03-08 | International Coal Refining Company | Coal Liquefaction desulfurization process |
| US4396488A (en) * | 1981-10-08 | 1983-08-02 | Electric Power Research Institute, Inc. | Process for coal liquefaction employing a superior coal liquefaction process solvent |
| US4411767A (en) * | 1982-09-30 | 1983-10-25 | Air Products And Chemicals, Inc. | Integrated process for the solvent refining of coal |
| US4428818A (en) * | 1982-12-07 | 1984-01-31 | Mobil Oil Corporation | Liquefaction of coal |
-
1983
- 1983-12-14 US US06/561,388 patent/US4547201A/en not_active Expired - Fee Related
-
1984
- 1984-10-26 CA CA000466392A patent/CA1243204A/en not_active Expired
- 1984-10-26 AU AU34727/84A patent/AU564513B2/en not_active Ceased
- 1984-11-02 ZA ZA848593A patent/ZA848593B/en unknown
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4133646A (en) * | 1976-10-18 | 1979-01-09 | Electric Power Research Institute, Inc. | Phenolic recycle solvent in two-stage coal liquefaction process |
| US4192653A (en) * | 1977-12-29 | 1980-03-11 | Gulf Research And Development Company | Novel fuel compositions comprising upgraded solid _and/or semi-solid material prepared from coal |
| US4203823A (en) * | 1978-07-03 | 1980-05-20 | Gulf Research & Development Company | Combined coal liquefaction-gasification process |
| US4276053A (en) * | 1978-12-13 | 1981-06-30 | The British Petroleum Company Limited | Fuel composition and method for its preparation |
| US4376032A (en) * | 1981-05-29 | 1983-03-08 | International Coal Refining Company | Coal Liquefaction desulfurization process |
| US4396488A (en) * | 1981-10-08 | 1983-08-02 | Electric Power Research Institute, Inc. | Process for coal liquefaction employing a superior coal liquefaction process solvent |
| US4411767A (en) * | 1982-09-30 | 1983-10-25 | Air Products And Chemicals, Inc. | Integrated process for the solvent refining of coal |
| US4428818A (en) * | 1982-12-07 | 1984-01-31 | Mobil Oil Corporation | Liquefaction of coal |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4692270A (en) * | 1984-02-14 | 1987-09-08 | Nippon Petrochemicals Company, Limited | Surface active agent |
| US6435164B1 (en) * | 2000-12-07 | 2002-08-20 | Ford Global Technologies, Inc. | Fuel weathering method for vehicle evaporative emission system |
| US20110180266A1 (en) * | 2008-06-30 | 2011-07-28 | A.P. Meller-Mærsk A/S | Drill ship for deep sea intervention operations |
| US20180037831A1 (en) * | 2015-02-10 | 2018-02-08 | Avantium Knowledge Centre B.V. | Fuel composition comprising humins |
| US10858601B2 (en) * | 2015-02-10 | 2020-12-08 | Avantium Knowledge Centre B.V. | Fuel composition comprising humins |
| CN109355083A (en) * | 2018-11-26 | 2019-02-19 | 中冶焦耐(大连)工程技术有限公司 | Process and system for extracting three-mixed fraction by tar reduced pressure distillation |
| CN109355083B (en) * | 2018-11-26 | 2024-05-14 | 中冶焦耐(大连)工程技术有限公司 | Process and system for extracting three-mixed fraction by reduced pressure distillation of tar |
Also Published As
| Publication number | Publication date |
|---|---|
| CA1243204A (en) | 1988-10-18 |
| AU3472784A (en) | 1985-06-20 |
| AU564513B2 (en) | 1987-08-13 |
| ZA848593B (en) | 1985-06-26 |
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